Fibers of polymer-wax compositions

ABSTRACT

Disposable article that include fibers formed from compositions comprising thermoplastic polymers and waxes are disclosed, where the wax is dispersed throughout the thermoplastic polymer.

FIELD OF THE INVENTION

In one aspect, the invention relates to fibers formed from compositionscomprising intimate admixtures of thermoplastic polymers and waxes.Another aspect of the invention also relates to methods of making thesecompositions.

BACKGROUND OF THE INVENTION

Thermoplastic polymers are used in a wide variety of applications.However, thermoplastic polymers, such as polypropylene and polyethylenepose additional challenges compared to other polymer species, especiallywith respect to formation of, for example, fibers. This is because thematerial and processing requirements for production of fibers are muchmore stringent than for producing other forms, for example, films. Forthe production of fibers, polymer melt flow characteristics are moredemanding on the material's physical and rheological properties vs otherpolymer processing methods. Also, the local extensional rate and shearrate are much greater in fiber production than other processes and, forspinning very fine fibers, small defects, slight inconsistencies, orphase incompatibilities in the melt are not acceptable for acommercially viable process. Moreover, high molecular weightthermoplastic polymers cannot be easily or effectively spun into finefibers. Given their availability and potential strength improvement, itwould be desirable to provide a way to easily and effectively spin suchhigh molecular weight polymers.

Most thermoplastic polymers, such as polyethylene, polypropylene, andpolyethylene terephthalate, are derived from monomers (e.g., ethylene,propylene, and terephthalic acid, respectively) that are obtained fromnon-renewable, fossil-based resources (e.g., petroleum, natural gas, andcoal). Thus, the price and availability of these resources ultimatelyhave a significant impact on the price of these polymers. As theworldwide price of these resources escalates, so does the price ofmaterials made from these polymers. Furthermore, many consumers displayan aversion to purchasing products that are derived solely frompetrochemicals, which are non-renewable fossil based resources. Otherconsumers may have adverse perceptions about products derived frompetrochemicals as being “unnatural” or not environmentally friendly.

Thermoplastic polymers are often incompatible with, or have poormiscibility with additives (e.g., waxes, pigments, organic dyes,perfumes, etc.) that might otherwise contribute to a reduced consumptionof these polymers in the manufacture of downstream articles. Heretofore,the art has not effectively addressed how to reduce the amount ofthermoplastic polymers derived from non-renewable, fossil-basedresources in the manufacture of common articles employing thesepolymers. Accordingly, it would be desirable to address this deficiency.Existing art has combined polypropylene with additives, withpolypropylene as the minor component to form cellular structures. Thesecellular structures are the purpose behind including renewable materialsthat are later removed or extracted after the structure is formed. U.S.Pat. No. 3,093,612 describes the combination of polypropylene withvarious fatty acids where the fatty acid is removed. The scientificpaper J. Apply. Polym. Sci 82 (1) pp. 169-177 (2001) discloses use ofdiluents on polypropylene for thermally induced phase separation toproduce an open and large cellular structure but at low polymer ratio,where the diluent is subsequently removed from the final structure. Thescientific paper J. Apply. Polym. Sci 105 (4) pp. 2000-2007 (2007)produces microporous membranes via thermally induced phase separationwith dibutyl phthalate and soy bean oil mixtures, with a minor componentof polypropylene. The diluent is removed in the final structure. Thescientific paper Journal of Membrane Science 108 (1-2) pp. 25-36 (1995)produces hollow fiber microporous membranes using soy bean oil andpolypropylene mixtures, with a minor component of polypropylene andusing thermally induced phase separation to produce the desired membranestructure. The diluent is removed in the final structure. In all ofthese cases, the diluent as described is removed to produce the finalstructure. These structures before the diluent is removed are oily withexcessive amounts of diluent to produce very open microporous structureswith pore sizes >10 μm.

There have been many attempts to make nonwoven articles. However,because of costs, the difficultly in processing, and end-use properties,there are only a limited number of options. Useful fibers for nonwovenarticles are difficult to produce and pose additional challengescompared to films and laminates. This is because the material andprocessing characteristics for fibers is much more stringent than forproducing films, blow-molding articles, and injection-molding articles.For the production of fibers, the processing time during structureformation is typically much shorter and flow characteristics are moredemanding on the material's physical and rheological characteristics.The local strain rate and shear rate are much greater in fiberproduction than other processes. Additionally, a homogeneous compositionis required for fiber spinning. For spinning very fine fibers, smalldefects, slight inconsistencies, or non-homogeneity in the melt are notacceptable for a commercially viable process. The more attenuated thefibers, the more critical the processing conditions and selection ofmaterials.

Thus, a need exists for fibers from compositions of thermoplasticpolymers that allow for use of higher molecular weight and/or decreasednon-renewable resource based materials, and/or incorporation of furtheradditives, such as perfumes and dyes. A still further need is for fibersfrom compositions that leave the additive present to deliver renewablematerials in the final product and that can also enable the addition offurther additives into the final structure, such as dyes and perfumes,for example.

SUMMARY OF THE INVENTION

In one aspect, the invention is directed to fibers produced by meltspinning compositions comprising an intimate admixture of athermoplastic polymer and a wax having a melting point greater than 25°C. The wax can have a melting point that is lower than the meltingtemperature of the thermoplastic polymer. The composition can be in theform of pellets produced to be used as-is or for storage for future use,for example to make fibers. Optionally, the composition can be furtherprocessed into the final usable form, such as fibers, films and moldedarticles. The fibers can have a diameter of less than 200 μm. The fiberscan be monocomponent or bicomponent, discrete and/or continuous, inaddition to being hollow, round, and/or shaped. The fiber can bethermally bondable.

The thermoplastic polymer can comprise a polyolefin, a polyester, apolyamide, copolymers thereof, or combinations thereof. Thethermoplastic polymer can be selected from the group consisting ofpolypropylene, polyethylene, polypropylene co-polymer, polyethyleneco-polymer, polyethylene terephthalate, polybutylene terephthalate,polylactic acid, polyhydroxyalkanoates, polyamide-6, polyamide-6,6, andcombinations thereof. Polypropylene having a melt flow index of greaterthan 0.5 g/10 min or of greater than 10 g/10 min can be used. Thepolypropylene can have a weight average molecular weight of about 20 kDato about 700 kDa. The thermoplastic polymer can be derived from arenewable bio-based feed stock origin, such as bio polyethylene or biopolypropylene, and/or can be recycled source, such as post consumer use.

The wax can be present in the composition in an amount of about 1 wt %to about 20 wt %, about 2 wt % to about 15 wt %, or about 3 wt % toabout 10 wt % based upon the total weight of the composition. The waxcan comprise a lipid, which can be selected from the group consisting ofa monoglyceride, diglyceride, triglyceride, fatty acid, fatty alcohol,esterified fatty acid, epoxidized lipid, maleated lipid, hydrogenatedlipid, alkyd resin derived from a lipid, sucrose polyester, orcombinations thereof. The wax can comprise a mineral wax, such as alinear alkane, a branched alkane, or combinations thereof. Specificexamples of mineral wax are paraffin and petrolatum. The wax can beselected from the group consisting of hydrogenated soy bean oil,partially hydrogenated soy bean oil, epoxidized soy bean oil, maleatedsoy bean oil, tristearin, tripalmitin, 1,2-dipalmitoolein,1,3-dipalmitoolein, 1-palmito-3-stearo-2-olein,1-palmito-2-stearo-3-olein, 2-palmito-1-stearo-3-olein,1,2-dipalmitolinolein, 1,2-distearo-olein, 1,3-distearo-olein,trimyristin, trilaurin, capric acid, caproic acid, caprylic acid, lauricacid, myristic acid, palmitic acid, stearic acid, and combinationsthereof. The wax can be selected from the group consisting of ahydrogenated plant oil, a partially hydrogenated plant oil, anepoxidized plant oil, a maleated plant oil. Specific examples of suchplant oils include soy bean oil, corn oil, canola oil, and palm kerneloil.

The wax can be dispersed within the thermoplastic polymer such that thewax has a droplet size of less than 2 μm, less than 1 μm, or less than500 nm within the thermoplastic polymer. The wax can be a renewablematerial.

The compositions disclosed herein can further comprise an additive. Theadditive can be oil soluble or oil dispersible. Examples of additivesinclude perfume, dye, pigment, nucleating agent, clarifying agent,anti-microbial agent, surfactant, nanoparticle, antistatic agent,filler, or combination thereof.

In another aspect, provided is a method of making a composition asdisclosed herein, the method comprising a) mixing the thermoplasticpolymer, in a molten state, with the wax, also in the molten state, toform the admixture; and b) cooling the admixture to a temperature at orless than the solidification temperature of the thermoplastic polymer in10 seconds or less to form the composition. The method of making acomposition can comprise a) melting a thermoplastic polymer to form amolten thermoplastic polymer; b) mixing the molten thermoplastic polymerand a wax to form an admixture; and c) cooling the admixture to atemperature at or less than the solidification temperature of thethermoplastic polymer in 10 seconds or less. The mixing can be at ashear rate of greater than 10 s⁻¹, or about 30 to about 100 s⁻¹. Theadmixture can be cooled in 10 seconds or less to a temperature of 50° C.or less. The composition can be pelletized. The pelletizing can occurafter cooling the admixture or before or simultaneous to cooling theadmixture. The composition can be made using an extruder, such as asingle- or twin-screw extruder. Alternatively, the method of making acomposition can comprise a) melting a thermoplastic polymer to form amolten thermoplastic polymer; b) mixing the molten thermoplastic polymerand a wax to form an admixture; and c) spinning the molten mixture toform filaments or fibers which solidify upon cooling.

BRIEF DESCRIPTION OF THE DRAWINGS

For a more complete understanding of the disclosure, reference should bemade to the following detailed description and accompanying drawingwherein:

FIG. 1 shows the viscosity of unmodified polypropylene and Examples 1-3,compositions as disclosed herein;

FIG. 2 shows scanning electron microscopy (SEM) images of unmodifiedpolypropylene (A) and Examples 1-3 (B-D), compositions as disclosedherein; and

FIG. 3 is a schematic representation of a disposable absorbent article.

FIGS. 4-6 show Table 1.

FIGS. 7 and 8 show Table 2.

FIGS. 9 and 10 show Table 3.

While the disclosed invention is susceptible of embodiments in variousforms, there are illustrated in the drawings (and will hereafter bedescribed) specific embodiments of the invention, with the understandingthat the disclosure is intended to be illustrative, and is not intendedto limit the invention to the specific embodiments described andillustrated herein.

DETAILED DESCRIPTION OF THE INVENTION

Fibers disclosed herein are made by melt spinning compositions of anintimate admixture of a thermoplastic polymer and a wax. The term“intimate admixture” refers to the physical relationship of the wax andthermoplastic polymer, wherein the wax is dispersed within thethermoplastic polymer. The droplet size of the wax within thethermoplastic polymer is a parameter that indicates the level ofdispersion of the wax within the thermoplastic polymer. The smaller thedroplet size, the higher the dispersion of the wax within thethermoplastic polymer, the larger the droplet size the lower thedispersion of the wax within the thermoplastic polymer. As used herein,the term “admixture” refers to the intimate admixture of the one of theinventions disclosed herein, and not an “admixture” in the more generalsense of a standard mixture of materials.

The droplet size of the wax within the thermoplastic polymer is lessthan 2 μm and can be less than 1 μm, or less than 500 nm. Othercontemplated droplet sizes of the wax dispersed within the thermoplasticpolymer include less than 1.5 μm, less than 900 nm, less than 800 nm,less than 700 nm, less than 600 nm, less than 400 nm, less than 300 nm,and less than 200 nm.

The droplet size of the wax can be measured by scanning electronmicroscopy (SEM) indirectly by measuring a void size in thethermoplastic polymer, after removal of the wax from the composition.Removal of the wax is typically performed prior to SEM imaging due toincompatibility of the wax and the SEM imaging technique. Thus, the voidmeasured by SEM imaging is correlated to the droplet size of the wax inthe composition, as exemplified in FIG. 2.

One exemplary way to achieve a suitable dispersion of the wax within thethermoplastic polymer is by admixing the thermoplastic polymer, in amolten state, and the wax. The thermoplastic polymer is melted (e.g.,exposed to temperatures greater than the thermoplastic polymer'ssolidification temperature) to provide the molten thermoplastic polymerand mixed with the wax. The thermoplastic polymer can be melted prior toaddition of the wax or can be melted in the presence of the wax. Itshould be understood that when the polymer is melted, the wax is also inthe molten state. The term wax hereafter can refer to the componenteither in the solid (optionally crystalline) state or in the moltenstate, depending on the temperature. It is not required that the wax besolidified at a temperature at which the polymer is solidified. Forexample, polypropylene is a semi-crystalline solid at 90° C., which isabove the melting point of many waxes.

The thermoplastic polymer and wax can be mixed, for example, at a shearrate of greater than 10s⁻¹. Other contemplated shear rates includegreater than 10, about 15 to about 1000, about 20 to about 200 or up to500 s⁻¹. The higher the shear rate of the mixing, the greater thedispersion of the wax in the composition as disclosed herein. Thus, thedispersion can be controlled by selecting a particular shear rate duringformation of the composition.

The wax and molten thermoplastic polymer can be mixed using anymechanical means capable of providing the necessary shear rate to resultin a composition as disclosed herein. Non-limiting examples ofmechanical means include a mixer, such as a Haake batch mixer, and anextruder (e.g., a single- or twin-screw extruder).

The mixture of molten thermoplastic polymer and wax is then rapidly(e.g., in less than 10 seconds) cooled to a temperature lower than thesolidification temperature (either via traditional thermoplastic polymercrystallization or passing below the polymer glass transitiontemperature) of the thermoplastic polymer. The admixture can be cooledto less than 200° C., less than 150° C., less than 100° C. less than 75°C., less than 50° C., less than 40° C., less than 30° C., less than 20°C., less than 15° C., less than 10° C., or to a temperature of about 0°C. to about 30° C., about 0° C. to about 20° C., or about 0° C. to about10° C. For example, the mixture can be placed in a low temperatureliquid (e.g., the liquid is at or below the temperature to which themixture is cooled) or gas. The liquid can be ambient or controlledtemperature water. The gas can be ambient air or controlled temperatureand humidity air. Any quenching media can be used so long as it coolsthe admixture rapidly. Additional liquids such as oils, alcohols andketones can be used for quenching, along with mixtures comprising water(sodium chloride for example) depending on the admixture composition.Additional gases can be used, such as carbon dioxide and nitrogen, orany other component naturally occurring in atmospheric temperature andpressure air.

Optionally, the composition is in the form of pellets. Pellets of thecomposition can be formed prior to, simultaneous to, or after cooling ofthe mixture. The pellets can be formed by strand cutting or underwaterpelletizing. In strand cutting, the composition is rapidly quenched(generally in a time period much less than 10 seconds) then cut intosmall pieces. In underwater pelletizing, the mixture is cut into smallpieces and simultaneously or immediately thereafter placed in thepresence of a low temperature liquid that rapidly cools and solidifiesthe mixture to form the pelletized composition. Such pelletizing methodsare well understood by the ordinarily skilled artisan. Pelletmorphologies can be round or cylindrical, and can have no dimensionlarger than 15 mm, more preferably less than 10 mm, or no dimensionlarger than 5 mm.

Alternatively, the admixture (admixture and mixture or usedinterchangeably here within this document) can be used whilst mixed inthe molten state and formed directly into fibers.

Thermoplastic Polymers

Thermoplastic polymers, as used in the disclosed compositions, arepolymers that melt and then, upon cooling, crystallize or harden, butcan be re-melted upon further heating. Suitable thermoplastic polymersused herein have a melting temperature from about 60° C. to about 300°C., from about 80° C. to about 250° C., or from 100° C. to 215° C.

The thermoplastic polymers can be derived from renewable resources orfrom fossil minerals and oils. The thermoplastic polymers derived fromrenewable resources are bio-based, for example such as bio producedethylene and propylene monomers used in the production polypropylene andpolyethylene. These material properties are essentially identical tofossil based product equivalents, except for the presence of carbon-14in the thermoplastic polymer. Renewable and fossil based thermoplasticpolymers can be combined together in any of the embodiments of theinvention disclosed herein in any ratio, depending on cost andavailability. Recycled thermoplastic polymers can also be used, alone orin combination with renewable and/or fossil derived thermoplasticpolymers. The recycled thermoplastic polymers can be pre-conditioned toremove any unwanted contaminants prior to compounding or they can beused during the compounding and extrusion process, as well as simplyleft in the admixture. These contaminants can include trace amounts ofother polymers, pulp, pigments, inorganic compounds, organic compoundsand other additives typically found in processed polymeric compositions.The contaminants should not negatively impact the final performanceproperties of the admixture, for example, causing spinning breaks duringa fiber spinning process.

The molecular weight of the thermoplastic polymer is sufficiently highto enable entanglement between polymer molecules and yet low enough tobe melt spinnable. Addition of the wax into the composition allows forcompositions containing higher molecular weight thermoplastic polymersto be spun, compared to compositions without a wax. Thus, suitablethermoplastic polymers can have weight average molecular weights ofabout 1000 kDa or less, about 5 kDa to about 800 kDa, about 10 kDa toabout 700 kDa, or about 20 kDa to about 400 kDa. The weight averagemolecular weight is determined by the specific method for each polymer,but is generally measured using either gel permeation chromatography(GPC) or from solution viscosity measurements. The thermoplastic polymerweight average molecular weight should be determined before additioninto the admixture.

Suitable thermoplastic polymers generally include polyolefins,polyesters, polyamides, copolymers thereof, and combinations thereof.The thermoplastic polymer can be selected from the group consisting ofpolypropylene, polyethylene, polypropylene co-polymer, polyethyleneco-polymer, polyethylene terephthalate, polybutylene terephthalate,polylactic acid, polyhydroxyalkanoates, polyamide-6, polyamide-6,6, andcombinations thereof.

More specifically, however, the thermoplastic polymers preferablyinclude polyolefins such as polyethylene or copolymers thereof,including low density, high density, linear low density, or ultra lowdensity polyethylenes such that the polyethylene density ranges between0.90 grams per cubic centimeter to 0.97 grams per cubic centimeter, mostpreferred between 0.92 and 0.95 grams per cubic centimeter. The densityof the polyethylene will is determined by the amount and type ofbranching and depends on the polymerization technology and comonomertype. Polypropylene and/or polypropylene copolymers, including atacticpolypropylene; isotactic polypropylene, syndiotactic polypropylene, andcombination thereof can also be used. Polypropylene copolymers,especially ethylene can be used to lower the melting temperature andimprove properties. These polypropylene polymers can be produced usingmetallocene and Ziegler-Natta catalyst systems. These polypropylene andpolyethylene compositions can be combined together to optimize end-useproperties. Polybutylene is also a useful polyolefin.

Other suitable polymers include polyamides or copolymers thereof, suchas Nylon 6, Nylon 11, Nylon 12, Nylon 46, Nylon 66; polyesters orcopolymers thereof, such as maleic anhydride polypropylene copolymer,polyethylene terephthalate; olefin carboxylic acid copolymers such asethylene/acrylic acid copolymer, ethylene/maleic acid copolymer,ethylene/methacrylic acid copolymer, ethylene/vinyl acetate copolymersor combinations thereof; polyacrylates, polymethacrylates, and theircopolymers such as poly(methyl methacrylates). Other nonlimitingexamples of polymers include polycarbonates, polyvinyl acetates,poly(oxymethylene), styrene copolymers, polyacrylates,polymethacrylates, poly(methyl methacrylates), polystyrene/methylmethacrylate copolymers, polyetherimides, polysulfones, or combinationsthereof. In some embodiments, thermoplastic polymers includepolypropylene, polyethylene, polyamides, polyvinyl alcohol, ethyleneacrylic acid, polyolefin carboxylic acid copolymers, polyesters, andcombinations thereof.

Biodegradable thermoplastic polymers also are contemplated for useherein. Biodegradable materials are susceptible to being assimilated bymicroorganisms, such as molds, fungi, and bacteria when thebiodegradable material is buried in the ground or otherwise contacts themicroorganisms (including contact under environmental conditionsconducive to the growth of the microorganisms). Suitable biodegradablepolymers also include those biodegradable materials which areenvironmentally-degradable using aerobic or anaerobic digestionprocedures, or by virtue of being exposed to environmental elements suchas sunlight, rain, moisture, wind, temperature, and the like. Thebiodegradable thermoplastic polymers can be used individually or as acombination of biodegradable or non-biodegradable polymers.Biodegradable polymers include polyesters containing aliphaticcomponents. Among the polyesters are ester polycondensates containingaliphatic constituents and poly(hydroxycarboxylic) acid. The esterpolycondensates include diacids/diol aliphatic polyesters such aspolybutylene succinate, polybutylene succinate co-adipate,aliphatic/aromatic polyesters such as terpolymers made of butylene diol,adipic acid and terephthalic acid. The poly(hydroxycarboxylic) acidsinclude lactic acid based homopolymers and copolymers,polyhydroxybutyrate (PHB), or other polyhydroxyalkanoate homopolymersand copolymers. Such polyhydroxyalkanoates include copolymers of PHBwith higher chain length monomers, such as C₆-C_(12,) and higher,polyhydroxyalkanaotes, such as those disclosed in U.S. Pat. Nos. Re.36,548 and 5,990,271.

An example of a suitable commercially available polylactic acid isNATUREWORKS from Cargill Dow and LACEA from Mitsui Chemical. An exampleof a suitable commercially available diacid/diol aliphatic polyester isthe polybutylene succinate/adipate copolymers sold as BIONOLLE 1000 andBIONOLLE 3000 from the Showa High Polymer Company, Ltd. (Tokyo, Japan).An example of a suitable commercially available aliphatic/aromaticcopolyester is the poly(tetramethylene adipate-co-terephthalate) sold asEASTAR BIO Copolyester from Eastman Chemical or ECOFLEX from BASF.

Non-limiting examples of suitable commercially available polypropyleneor polypropylene copolymers include Basell Profax PH-835 (a 35 melt flowrate Ziegler-Natta isotactic polypropylene from Lyondell-Basell), BasellMetocene MF-650W (a 500 melt flow rate metallocene isotacticpolypropylene from Lyondell-Basell), Polybond 3200 (a 250 melt flow ratemaleic anhydride polypropylene copolymer from Crompton), Exxon Achieve3854 (a 25 melt flow rate metallocene isotactic polypropylene fromExxon-Mobil Chemical), and Mosten NB425 (a 25 melt flow rateZiegler-Natta isotactic polypropylene from Unipetrol). Other suitablepolymer may include Danimer 27510 (a polyhydroxyalkanoate polypropylenefrom Danimer Scientific LLC), Dow Aspun 6811A (a 27 melt indexpolyethylene octene copolymer from Dow Chemical), and Eastman 9921 (apolyester terephthalic homopolymer with a nominally 0.81 intrinsicviscosity from Eastman Chemical).

The thermoplastic polymer component can be a single polymer species asdescribed above or a blend of two or more thermoplastic polymers asdescribed above.

If the polymer is polypropylene, the thermoplastic polymer can have amelt flow index of greater than 0.5 g/10 min, as measured by ASTMD-1238, used for measuring polypropylene. Other contemplated melt flowindices include greater than 5 g/10 min, greater than 10 g/10 min, orabout 5 g/10 min to about 50 g/10 min.

Waxes

A wax, as used in the disclosed composition, is a lipid, mineral wax, orcombination thereof, wherein the lipid, mineral wax, or combinationthereof has a melting point of greater than 25° C. More preferred is amelting point above 35° C., still more preferred above 45° C. and mostpreferred above 50° C. The wax can have a melting point that is lowerthan the melting temperature of the thermoplastic polymer in thecomposition. The terms “wax” and “oil” are differentiated bycrystallinity of the component at or near 25° C. In all cases, the “wax”will have a maximum melting temperature less than the thermoplasticpolymer, preferably less than 100° C. and most preferably less than 80°C. The wax can be a lipid. The lipid can be a monoglyceride,diglyceride, triglyceride, fatty acid, fatty alcohol, esterified fattyacid, epoxidized lipid, maleated lipid, hydrogenated lipid, alkyd resinderived from a lipid, sucrose polyester, or combinations thereof. Themineral wax can be a linear alkane, a branched alkane, or combinationsthereof. The waxes can be partially or fully hydrogenated materials, orcombinations and mixtures thereof, that were formally liquids at roomtemperature in their unmodified forms. When the temperature is above themelting temperature of the wax, it is a liquid oil. When in the moltenstate, the wax can be referred to as an “oil”. The terms “wax” and “oil”only have meaning when measured at 25° C. The wax will be a solid at 25°C., while an oil is not a solid at 25° C. Otherwise they are usedinterchangeably above 25° C.

Because the wax may contain a distribution of melting temperatures togenerate a peak melting temperature, the wax melting temperature isdefined as having a peak melting temperature 25° C. or above as definedas when >50 weight percent of the wax component melts at or above 25° C.This measurement can be made using a differential scanning calorimeter(DSC), where the heat of fusion is equated to the weight percentfraction of the wax.

The wax number average molecular weight, as determined by gel permeationchromatography (GPC), should be less than 2 kDa, preferably less than1.5 kDa, still more preferred less than 1.2 kDa.

The amount of wax is determined via gravimetric weight loss method. Thesolidified mixture is placed, with the narrowest specimen dimension nogreater than 1 mm, into acetone at a ratio of 1 g or mixture per 100 gof acetone using a refluxing flask system. First the mixture is weighedbefore being placed into the reflux flask, and then the acetone andmixtures are heated to 60° C. for 20 hours. The sample is removed andair dried for 60 minutes and a final weight determined. The equation forcalculating the weight percent wax isweight % wax=([initial mass-final mass]/[initial mass])×100%

Non-limiting examples of waxes contemplated in the compositionsdisclosed herein include beef tallow, castor wax, coconut wax, coconutseed wax, corn germ wax, cottonseed wax, fish wax, linseed wax, olivewax, oiticica wax, palm kernel wax, palm wax, palm seed wax, peanut wax,rapeseed wax, safflower wax, soybean wax, sperm wax, sunflower seed wax,tall wax, tung wax, whale wax, and combinations thereof. Non-limitingexamples of specific triglycerides include triglycerides such as, forexample, tristearin, tripalmitin, 1,2-dipalmitoolein,1,3-dipalmitoolein, 1-palmito-3-stearo-2-olein,1-palmito-2-stearo-3-olein, 2-palmito-1-stearo-3-olein,1,2-dipalmitolinolein, 1,2-distearo-olein, 1,3-distearo-olein,trimyristin, trilaurin and combinations thereof. Non-limiting examplesof specific fatty acids contemplated include capric acid, caproic acid,caprylic acid, lauric acid, myristic acid, palmitic acid, stearic acid,and mixtures thereof. Other specific waxes contemplated includehydrogenated soy bean oil, partially hydrogenated soy bean oil,partially hydrogenated palm kernel oil, and combinations thereof.Inedible waxes from Jatropha and rapeseed oil can also be used. The waxcan be selected from the group consisting of a hydrogenated plant oil, apartially hydrogenated plant oil, an epoxidized plant oil, a maleatedplant oil. Specific examples of such plant oils include soy bean oil,corn oil, canola oil, and palm kernel oil. Specific examples of mineralwax include paraffin (including petrolatum), Montan wax, as well aspolyolefin waxes produced from cracking processes, preferentiallypolyethylene derived waxes. Mineral waxes and plant derived waxes can becombined together. Plant based waxes can be differentiated by theircarbon-14 content.

The wax can be from a renewable material (e.g., derived from a renewableresource). As used herein, a “renewable resource” is one that isproduced by a natural process at a rate comparable to its rate ofconsumption (e.g., within a 100 year time frame). The resource can bereplenished naturally, or via agricultural techniques. Non-limitingexamples of renewable resources include plants (e.g., sugar cane, beets,corn, potatoes, citrus fruit, woody plants, lignocellulosics,hemicellulosics, cellulosic waste), animals, fish, bacteria, fungi, andforestry products. These resources can be naturally occurring, hybrids,or genetically engineered organisms. Natural resources such as crudeoil, coal, natural gas, and peat, which take longer than 100 years toform, are not considered renewable resources.

The wax, as disclosed herein, can be present in the composition at aweight percent of 1 wt % to 20 wt %, based upon the total weight of thecomposition. Other contemplated wt % ranges of the wax include 2 wt % to15 wt %, with a preferred range from about 3 wt % to about 10 wt %.Specific wax wt % contemplated include about 1 wt %, 2 wt %, 3 wt %, 4wt %, 5 wt %, about 6 wt %, about 7 wt %, about 8 wt %, about 9 wt %,about 10 wt %, about 11 wt %, about 12 wt %, about 13 wt %, about 14 wt%, about 15 wt %, about 16 wt %, about 17 wt %, about 18 wt %, about 19wt %, and about 20 wt, based upon the total weight of the composition.

Additives

The compositions disclosed herein can further include an additive. Theadditive can be dispersed throughout the composition, or can besubstantially in the thermoplastic polymer portion of the thermoplasticlayer or substantially in the wax portion of the composition. In caseswhere the additive is in the wax portion of the composition, theadditive can be wax soluble or wax dispersible.

Non-limiting examples of classes of additives contemplated in thecompositions disclosed herein include perfumes, dyes, pigments,nanoparticles, antistatic agents, fillers, and combinations thereof. Thecompositions disclosed herein can contain a single additive or a mixtureof additives. For example, both a perfume and a colorant (e.g., pigmentand/or dye) can be present in the composition. The additive(s), whenpresent, is/are present in a weight percent of 0.05 wt % to 20 wt %, or0.1 wt % to 10 wt %. Specifically contemplated weight percentagesinclude 0.5 wt %, 0.6 wt %, 0.7 wt %, 0.8 wt %, 0.9 wt %, 1 wt %, 1.1 wt%, 1.2 wt %, 1.3 wt %, 1.4 wt %, 1.5 wt %, 1.6 wt %, 1.7 wt %, 1.8 wt %,1.9 wt %, 2 wt %, 2.1 wt %, 2.2 wt %, 2.3 wt %, 2.4 wt %, 2.5 wt %, 2.6wt %, 2.7 wt %, 2.8 wt %, 2.9 wt %, 3 wt %, 3.1 wt %, 3.2 wt %, 3.3 wt%, 3.4 wt %, 3.5 wt %, 3.6 wt %, 3.7 wt %, 3.8 wt %, 3.9 wt %, 4 wt %,4.1 wt %, 4.2 wt %, 4.3 wt %, 4.4 wt %, 4.5 wt %, 4.6 wt %, 4.7 wt %,4.8 wt %, 4.9 wt %, 5 wt %, 5.1 wt %, 5.2 wt %, 5.3 wt %, 5.4 wt %, 5.5wt %, 5.6 wt %, 5.7 wt %, 5.8 wt %, 5.9 wt %, 6 wt %, 6.1 wt %, 6.2 wt%, 6.3 wt %, 6.4 wt %, 6.5 wt %, 6.6 wt %, 6.7 wt %, 6.8 wt %, 6.9 wt %,7 wt %, 7.1 wt %, 7.2 wt %, 7.3 wt %, 7.4 wt %, 7.5 wt %, 7.6 wt %, 7.7wt %, 7.8 wt %, 7.9 wt %, 8 wt %, 8.1 wt %, 8.2 wt %, 8.3 wt %, 8.4 wt%, 8.5 wt %, 8.6 wt %, 8.7 wt %, 8.8 wt %, 8.9 wt %, 9 wt %, 9.1 wt %,9.2 wt %, 9.3 wt %, 9.4 wt %, 9.5 wt %, 9.6 wt %, 9.7 wt %, 9.8 wt %,9.9 wt %, and 10 wt %.

As used herein the term “perfume” is used to indicate any odoriferousmaterial that is subsequently released from the composition as disclosedherein. A wide variety of chemicals are known for perfume uses,including materials such as aldehydes, ketones, alcohols, and esters.More commonly, naturally occurring plant and animal oils and exudatesincluding complex mixtures of various chemical components are known foruse as perfumes. The perfumes herein can be relatively simple in theircompositions or can include highly sophisticated complex mixtures ofnatural and synthetic chemical components, all chosen to provide anydesired odor. Typical perfumes can include, for example, woody/earthybases containing exotic materials, such as sandalwood, civet andpatchouli oil. The perfumes can be of a light floral fragrance (e.g.rose extract, violet extract, and lilac). The perfumes can also beformulated to provide desirable fruity odors, e.g. lime, lemon, andorange. The perfumes delivered in the compositions and articlesdisclosed herein can be selected for an aromatherapy effect, such asproviding a relaxing or invigorating mood. As such, any material thatexudes a pleasant or otherwise desirable odor can be used as a perfumeactive in the compositions and articles disclosed herein.

A pigment or dye can be inorganic, organic, or a combination thereof.Specific examples of pigments and dyes contemplated include pigmentYellow (C.I. 14), pigment Red (C.I. 48:3), pigment Blue (C.I. 15:4),pigment Black (C.I. 7), and combinations thereof. Specific contemplateddyes include water soluble ink colorants like direct dyes, acid dyes,base dyes, and various solvent soluble dyes. Examples include, but arenot limited to, FD&C Blue 1 (C.I. 42090:2), D&C Red 6(C.I. 15850), D&CRed 7(C.I. 15850:1), D&C Red 9(C.I. 15585:1), D&C Red 21(C.I. 45380:2),D&C Red 22(C.I. 45380:3), D&C Red 27(C.I. 45410:1), D&C Red 28(C.I.45410:2), D&C Red 30(C.I. 73360), D&C Red 33(C.I. 17200), D&C Red34(C.I. 15880:1), and FD&C Yellow 5(C.I. 19140:1), FD&C Yellow 6(C.I.15985:1), FD&C Yellow 10(C.I. 47005:1), D&C Orange 5(C.I. 45370:2), andcombinations thereof.

Contemplated fillers include, but are not limited to inorganic fillerssuch as, for example, the oxides of magnesium, aluminum, silicon, andtitanium. These materials can be added as inexpensive fillers orprocessing aides. Other inorganic materials that can function as fillersinclude hydrous magnesium silicate, titanium dioxide, calcium carbonate,clay, chalk, boron nitride, limestone, diatomaceous earth, mica glassquartz, and ceramics. Additionally, inorganic salts, including alkalimetal salts, alkaline earth metal salts, phosphate salts, can be used.Additionally, alkyd resins can also be added to the composition. Alkydresins comprise a polyol, a polyacid or anhydride, and/or a fatty acid.

Additional contemplated additives include nucleating and clarifyingagents for the thermoplastic polymer. Specific examples, suitable forpolypropylene, for example, are benzoic acid and derivatives (e.g.sodium benzoate and lithium benzoate), as well as kaolin, talc and zincglycerolate. Dibenzlidene sorbitol (DBS) is an example of a clarifyingagent that can be used. Other nucleating agents that can be used areorganocarboxylic acid salts, sodium phosphate and metal salts (forexample aluminum dibenzoate) The nucleating or clarifying agents can beadded in ranges from 20 parts per million (20ppm) to 20,000 ppm, morepreferred range of 200 ppm to 2000 ppm and the most preferred range from1000 ppm to 1500 ppm. The addition of the nucleating agent can be usedto improve the tensile and impact properties of the finished admixturecomposition.

Contemplated surfactants include anionic surfactants, amphotericsurfactants, or a combination of anionic and amphoteric surfactants, andcombinations thereof, such as surfactants disclosed, for example, inU.S. Pat. Nos. 3,929,678 and 4,259,217 and in EP 414 549, WO93/08876 andWO93/08874.

Contemplated nanoparticles include metals, metal oxides, allotropes ofcarbon, clays, organically modified clays, sulfates, nitrides,hydroxides, oxy/hydroxides, particulate water-insoluble polymers,silicates, phosphates and carbonates. Examples include silicon dioxide,carbon black, graphite, grapheme, fullerenes, expanded graphite, carbonnanotubes, talc, calcium carbonate, betonite, montmorillonite, kaolin,zinc glycerolate, silica, aluminosilicates, boron nitride, aluminumnitride, barium sulfate, calcium sulfate, antimony oxide, feldspar,mica, nickel, copper, iron, cobalt, steel, gold, silver, platinum,aluminum, wollastonite, aluminum oxide, zirconium oxide, titaniumdioxide, cerium oxide, zinc oxide, magnesium oxide, tin oxide, ironoxides (Fe₂O₃, Fe₃O₄) and mixtures thereof. Nanoparticles can increasestrength, thermal stability, and/or abrasion resistance of thecompositions disclosed herein, and can give the compositions electricproperties.

It is contemplated to add oils or that some amount of oil is present inthe composition. The oil may be unrelated to the lipid present or can bean unsaturated or less saturated version of the wax lipid. The amount ofoil present can range from 0 weight percent to 40 weight percent of thecomposition, more preferably from 5 weight percent to 20 weight percentof the composition and most preferably from 8 weight percent to 15weight percent of the composition.

Contemplated anti-static agents include fabric softeners which are knownto provide antistatic benefits. For example those fabric softeners thathave a fatty acyl group which has an iodine value of above 20, such asN,N-di(tallowoyl-oxy-ethyl)-N,N-dimethyl ammonium methylsulfate.

Fibers

In one embodiment, the fibers may be monocomponent or multicomponent.The term “fiber” is defined as a solidified polymer shape with a lengthto thickness ratio of greater than 1,000. The monocomponent fibers mayalso be multiconstituent. Constituent, as used herein, is defined asmeaning the chemical species of matter or the material. Multiconstituentfiber, as used herein, is defined to mean a fiber containing more thanone chemical species or material. Multiconstituent and alloyed polymershave the same meaning herein and can be used interchangeably. Generally,fibers may be of monocomponent or multicomponent types. Component, asused herein, is defined as a separate part of the fiber that has aspatial relationship to another part of the fiber. The termmulticomponent, as used herein, is defined as a fiber having more thanone separate part in spatial relationship to one another. The termmulticomponent includes bicomponent, which is defined as a fiber havingtwo separate parts in a spatial relationship to one another. Thedifferent components of multicomponent fibers are arranged insubstantially distinct regions across the cross-section of the fiber andextend continuously along the length of the fiber. Methods for makingmulticomponent fibers are well known in the art. Multicomponent fiberextrusion was well known in the 1960's. DuPont was a lead technologydeveloper of multicomponent capability, with U.S. Pat. No. 3,244,785 andU.S. Pat. No. 3,704,971 providing a technology description of thetechnology used to make these fibers. “Bicomponent Fibers” by R.Jeffries from Merrow Publishing in 1971 laid a solid groundwork forbicomponent technology. More recent publications include “Taylor-MadePolypropylene and Bicomponent Fibers for the Nonwoven Industry,” TappiJournal December 1991 (p103) and “Advanced Fiber Spinning Technology”edited by Nakajima from Woodhead Publishing.

The nonwoven fabric disclosed herein may contain multiple types ofmonocomponent fibers that are delivered from different extrusion systemsthrough the same spinneret. The extrusion system, in this example, is amulticomponent extrusion system that delivers different polymers toseparate capillaries. For instance, one extrusion system would deliverpolypropylene with wax and the other a polypropylene copolymer such thatthe copolymer composition melts at different temperatures. In a secondexample, one extrusion system might deliver a polyethylene resin and theother polypropylene with wax. In a third example, one extrusion systemmight deliver a polypropylene resin with 30 weight percent wax and theother a polypropylene resin with 30 weight percent wax that has amolecular weight different from the first polypropylene resin. Thepolymer ratios in this system can range from 95:5 to 5:95, preferablyfrom 90:10 to 10:90 and 80:20 to 20:80.

Bicomponent and multicomponent fibers may be in a side-by-side,sheath-core (symmetric and eccentric), segmented pie, ribbon,islands-in-the-sea configuration, or any combination thereof. The sheathmay be continuous or non-continuous around the core. Non-inclusiveexamples of exemplarily multicomponent fibers are disclosed in U.S. Pat.No. 6,746,766. The ratio of the weight of the sheath to the core is fromabout 5:95 to about 95:5. The fibers disclosed herein may have differentgeometries that include, but are not limited to; round, elliptical, starshaped, trilobal, multilobal with 3-8 lobes, rectangular, H-shaped,C-shaped, I-shape, U-shaped and other various eccentricities. Hollowfibers can also be used. Preferred shapes are round, trilobal andH-shaped. The round and trilobal fiber shapes can also be hollow.

Sheath and core bicomponent fibers are preferred. In one preferred case,the component in the core may contain the thermoplastic polymer and wax,while the sheath does not. In this case the exposure to wax at thesurface of the fiber is reduced or eliminated. In another preferredcase, the sheath may contain the wax and the core does not. In this casethe concentration of wax at the fiber surface is higher than in thecore. Using sheath and core bicomponent fibers, the concentration of thewax can be selected to impart desired properties either in the sheath orcore, or some concentration gradient. It should be understood thatislands-in-a-sea bicomponent fibers are considered to be a type ofsheath and core fiber, but with multiple cores. Segmented pie fibers(hollow and solid) are contemplated. For one example, to split regionsthat contain wax from regions that do not contain wax using segmentedpie type of bicomponent fiber design. Splitting may occur duringmechanical deformation, application of hydrodynamic forces or othersuitable processes.

Tricomponent fibers are also contemplated. One example of a usefultricomponent fiber would be a three layered sheath/sheath/core fiber,where each component contains a different amount of wax. Differentamounts of wax in each layer may provide additional benefits. Forexample, the core can be a blend of 10 melt flow polypropylene with 30weight percent wax. The middle layer sheath may be a blend of 25 meltflow polypropylene with 20 weight percent wax and the outer layer may bestraight 35 melt flow rate polypropylene. It is preferred that the waxcontent between each layer is less than 40 wt %, more preferably lessthan 20 wt %. Another type of useful tricomponent fiber contemplated isa segmented pie type bicomponent design that also has a sheath.

A “highly attenuated fiber” is defined as a fiber having a high drawdown ratio. The total fiber draw down ratio is defined as the ratio ofthe fiber at its maximum diameter (which is typically resultsimmediately after exiting the capillary) to the final fiber diameter inits end use. The total fiber draw down ratio will be greater than 1.5,preferable greater than 5, more preferably greater than 10, and mostpreferably greater than 12. This is necessary to achieve the tactileproperties and useful mechanical properties.

The fiber will have a diameter of less than 50 μm. The diameter of thefibers made with any of the previously discussed compositions can be aslow as 0.1 μm if the mixture is being used to produce fine fibers. Thefibers can be either essentially continuous or essentiallydiscontinuous. Fibers commonly used to make spunbond nonwovens that aremade with any of the previously discussed compositions will have adiameter of from 5 μm to 30 μm, more preferably from 10 μm to 20 μm andmost preferred from 12 μm to about 18 μm. Fine fiber diameter will havea diameter from 0.1 μm to 5 μm, preferably from 0.2 μm to 3 μm and mostpreferred from 0.3 μm to 2 μm Fiber diameter is controlled by diegeometry, spinning speed or drawing speed, mass through-put, and blendcomposition and rheology. The fibers as described herein can beenvironmentally degradable.

The fibers described herein are typically used to make disposablearticles that include at least one layer of fibers made with any of thecompositions previously discussed, and which can be in the form of anonwoven material. The articles can be flushable. The term “flushable”as used herein refers to materials which are capable of dissolving,dispersing, disintegrating, and/or decomposing in a septic disposalsystem such as a toilet to provide clearance when flushed down thetoilet without clogging the toilet or any other sewage drainage pipe.The fibers and resulting articles may also be aqueous responsive. Theterm aqueous responsive as used herein means that when placed in wateror flushed, an observable and measurable change will result. Typicalobservations include noting that the article swells, pulls apart,dissolves, or observing a general weakened structure.

The hydrophilicity and hydrophobicity of the fibers can be adjusted asneeded. The base resin properties can have hydrophilic properties viacopolymerization (such as the case for certain polyesters (EASTONE fromEastman Chemical, the sulfopolyester family of polymers in general) orpolyolefins such as polypropylene or polyethylene) or have materialsadded to the base resin to render it hydrophilic. Exemplarily examplesof additives include CIBA Irgasurf® family of additives. The fibers inthe present invention can also be treated or coated after they are madeto render them hydrophilic. In the present invention, durablehydrophilicity is preferred. Durable hydrophilicity is defined asmaintaining hydrophilic characteristics after more than one fluidinteraction. For example, if the sample being evaluated is tested fordurable hydrophilicity, water can be poured on the sample and wettingobserved. If the sample wets out it is initially hydrophilic. The sampleis then completely rinsed with water and dried. The rinsing is best doneby putting the sample in a large container and agitating for ten secondsand then drying. The sample after drying should also wet out whencontacted again with water.

After the fiber is formed, the fiber may further be treated or thebonded fabric can be treated. A hydrophilic or hydrophobic finish can beadded to adjust the surface energy and chemical nature of the fabric.For example, fibers that are hydrophobic may be treated with wettingagents to facilitate absorption of aqueous liquids. A bonded fabric canalso be treated with a topical solution containing surfactants,pigments, slip agents, salt, or other materials to further adjust thesurface properties of the fiber.

In one embodiment, the fibers can be crimped, although it can bepreferred that they are not crimped. Crimped fibers are generallyproduced in two methods. The first method is mechanical deformation ofthe fiber after it is already spun. Fibers are melt spun, drawn down tothe final filament diameter and mechanically treated, generally throughgears or a stuffer box that imparts either a two dimensional or threedimensional crimp. This method is used in producing most carded staplefibers. The second method for crimping fibers is to extrudemulticomponent fibers that are capable of crimping in a spunlaidprocess. One of ordinary skill in the art would recognize that a numberof methods of making bicomponent crimped spunbond fibers exists;however, three main techniques are considered for making crimpedspunlaid nonwovens. The first is crimping that occurs in the spinlinedue to differential polymer crystallization in the spinline, a result ofdifferences in polymer type, polymer molecular weight characteristics(e.g., molecular weight distribution) or additives content. A secondmethod is differential shrinkage of the fibers after they have been spuninto a spunlaid substrate. For instance, heating the spunlaid web cancause fibers to shrink due to differences in crystallinity in theas-spun fibers, for example during the thermal bonding process. A thirdmethod of causing crimping is to mechanically stretch the fibers orspunlaid web (generally for mechanical stretching the web has beenbonded together). The mechanical stretching can expose differences inthe stress-strain curve between the two polymer components, which cancause crimping.

The tensile strength of a fiber is approximately greater than 25 MegaPascal (MPa). The fibers as disclosed herein have a tensile strength ofgreater than about 50 MPa, preferably greater than about 75 MPa, andmore preferably greater than about 100 MPa. Tensile strength is measuredusing an Instron following a procedure described by ASTM standard D3822-91 or an equivalent test.

The fibers as disclosed herein are not brittle and have a toughness ofgreater than 2 MPa, greater than 50 MPa, or greater than 100 MPa.Toughness is defined as the area under the stress-strain curve where thespecimen gauge length is 25 mm with a strain rate of 50 mm per minute.Elasticity or extensibility of the fibers may also be desired.

The fibers as disclosed herein can be thermally bondable if sufficientthermoplastic polymers are present in the fiber or on the outsidecomponent of the fiber (i.e. sheath of a bicomponent). Thermallybondable fibers are best used in the pressurized heat and thru-air heatbonding methods. Thermally bondable is typically achieved when thecomposition is present at a level of greater than about 15%, preferablygreater than about 30%, most preferably greater than about 40%, and mostpreferably greater than about 50% by weight of the fiber.

The fibers disclosed herein can be environmentally degradable dependingupon the amount of the composition that is present and the specificconfiguration of the fiber. “Environmentally degradable” is defined asbeing biodegradable, disintigratable, dispersible, flushable, orcompostable or a combination thereof. The fibers, nonwoven webs, andarticles can be environmentally degradable. As a result, the fibers maybe easily and safely disposed of either in existing compostingfacilities or may be flushable and can be safely flushed down the drainwithout detrimental consequences to existing sewage infrastructuresystems. The flushability of the fibers when used in disposable productssuch as wipes and feminine hygiene items offer additional convenienceand discretion to the consumer.

The term “biodegradable” refers to matter that, when exposed to anaerobic and/or anaerobic environment, is eventually reduced to monomericcomponents due to microbial, hydrolytic, and/or chemical actions. Underaerobic conditions, biodegradation leads to the transformation of thematerial into end products such as carbon dioxide and water. Underanaerobic conditions, biodegradation leads to the transformation of thematerials into carbon dioxide, water, and methane. The biodegradabilityprocess is often described as mineralization. Biodegradability meansthat all organic constituents of the matter (e.g., fibers) are subjectto decomposition eventually through biological activity.

There are a variety of different standardized biodegradability methodsthat have been established over time by various organizations and indifferent countries. Although the tests vary in the specific testingconditions, assessment methods, and criteria desired, there isreasonable convergence between different protocols so that they arelikely to lead to similar conclusions for most materials. For aerobicbiodegrability, the American Society for Testing and Materials (ASTM)has established ASTM D 5338-92: Test methods for Determining AerobicBiodegradation of Plastic Materials under Controlled CompostingConditions. The ASTM test measures the percent of test material thatmineralizes as a function of time by monitoring the amount of carbondioxide being released as a result of assimilation by microorganisms inthe presence of active compost held at a thermophilic temperature of 58°C. Carbon dioxide production testing may be conducted via electrolyticrespirometry. Other standard protocols, such 301B from the Organizationfor Economic Cooperation and Development (OECD), may also be used.Standard biodegradation tests in the absence of oxygen are described invarious protocols such as ASTM D 5511-94. These tests are used tosimulate the biodegradability of materials in an anaerobic solid-wastetreatment facility or sanitary landfill. However, these conditions areless relevant for the type of disposable applications that are describedfor the fibers and nonwovens as described herein.

Disintegration occurs when the fibrous substrate has the ability torapidly fragment and break down into fractions small enough not to bedistinguishable after screening when composted or to cause drainpipeclogging when flushed. A disintegratable material will also beflushable. Most protocols for disintegradability measure the weight lossof test materials over time when exposed to various matrices. Bothaerobic and anaerobic disintegration tests are used. Weight loss isdetermined by the amount of fibrous test material that is no longercollected on an 18 mesh sieve with 1 millimeter openings after thematerials is exposed to wastewater and sludge. For disintegration, thedifference in the weight of the initial sample and the dried weight ofthe sample recovered on a screen will determine the rate and extent ofdisintegration. The testing for biodegradability and disintegration arevery similar as a very similar environment, or the same environment,will be used for testing. To determine disintegration, the weight of thematerial remaining is measured while for biodegradability, the evolvedgases are measured. The fibers disclosed herein can rapidlydisintegrate.

The fibers as disclosed herein can also be compostable. ASTM hasdeveloped test methods and specifications for compostability. The testmeasures three characteristics: biodegradability, disintegration, andlack of ecotoxicity. Tests to measure biodegradability anddisintegration are described above. To meet the biodegradabilitycriteria for compostability, the material must achieve at least about60% conversion to carbon dioxide within 40 days. For the disintegrationcriteria, the material must have less than 10% of the test materialremain on a 2 millimeter screen in the actual shape and thickness thatit would have in the disposed product. To determine the last criteria,lack of ecotoxicity, the biodegradation byproducts must not exhibit anegative impact on seed germination and plant growth. One test for thiscriteria is detailed in OECD 208. The International BiodegradableProducts Institute will issue a logo for compostability once a productis verified to meet ASTM 6400-99 specifications. The protocol followsGermany's DIN 54900 which determine the maximum thickness of anymaterial that allows complete decomposition within one composting cycle.

The fibers described herein can be used to make disposable nonwovenarticles. The articles are commonly flushable. The term “flushable” asused herein refers to materials which are capable of dissolving,dispersing, disintegrating, and/or decomposing in a septic disposalsystem such as a toilet to provide clearance when flushed down thetoilet without clogging the toilet or any other sewage drainage pipe.The fibers and resulting articles may also be aqueous responsive. Theterm aqueous responsive as used herein means that when placed in wateror flushed, an observable and measurable change will result. Typicalobservations include noting that the article swells, pulls apart,dissolves, or observing a general weakened structure.

The nonwoven products produced from the fibers exhibit certainmechanical properties, particularly, strength, flexibility, softness,and absorbency. Measures of strength include dry and/or wet tensilestrength. Flexibility is related to stiffness and can attribute tosoftness. Softness is generally described as a physiologically perceivedattribute which is related to both flexibility and texture. Absorbencyrelates to the products' ability to take up fluids as well as thecapacity to retain them.

Configuration of the Fibers

The fibers disclosed herein can also be splittable fibers. Rheological,thermal, and solidification differential behavior can potentially causesplitting. Splitting may also occur by a mechanical means such as ringrolling, stress or strain, use of an abrasive, or differentialstretching, and/or by fluid induced distortion, such as hydrodynamic oraerodynamic.

For a bicomponent fiber, a composition as disclosed herein can be boththe sheath and the core with one of the components containing more waxand/or additives than the other component. Alternatively, thecomposition disclosed herein can be the sheath with the core being someother materials, e.g., pure polymer. The composition can alternativelybe the core with the sheath being some other polymer, e.g., purepolymer. The exact configuration of the fiber desired is dependent uponthe use of the fiber.

Processes of Making the Compositions as Disclosed Herein

Melt mixing of the polymer and wax: The polymer and wax can be suitablymixed by melting the polymer in the presence of the wax. In the meltstate, the polymer and wax are subjected to shear which enables adispersion of the oil into the polymer. In the melt state, the wax andpolymer are significantly more compatible with each other.

The melt mixing of the polymer and wax can be accomplished in a numberof different processes, but processes with high shear are preferred togenerate the preferred morphology of the composition. The processes caninvolve traditional thermoplastic polymer processing equipment. Thegeneral process order involves adding the polymer to the system, meltingthe polymer, and then adding the wax. However, the materials can beadded in any order, depending on the nature of the specific mixingsystem.

Haake Batch Mixer: A Haake Batch mixer is a simple mixing system withlow amount of shear and mixing. The unit is composed of two mixingscrews contained within a heated, fixed volume chamber. The materialsare added into the top of the unit as desired. The preferred order is toadd the polymer, heat to 20° C. to 120° C. above the polymer's melting(or solidification) temperature into the chamber first. Once the polymeris melted, the wax can be added and mixed with the molten polymer oncethe wax melts. The mixture is then mixed in the melt with the two mixingscrews for about 5 to about 15 minutes at screw RPM from about 60 toabout 120. Once the composition is mixed, the front of the unit isremoved and the mixed composition is removed in the molten state. By itsdesign, this system leaves parts of the composition at elevatedtemperatures before crystallization starts for several minutes. Thismixing process provides an intermediate quenching process, where thecomposition can take about 30 seconds to about 2 minutes to cool downand solidify. Mixture of polypropylene with hydrogenated soy bean oil inthe Haake mixture shows that greater than 20 wt % of molten wax leads toincomplete incorporation of the wax in the polypropylene mixture,indicating that higher shear rates can lead to better incorporation ofwax and greater amounts of wax able to be incorporated.

Single Screw Extruder: A single screw extruder is a typical process unitused in most molten polymer extrusion. The single screw extrudertypically includes a single shaft within a barrel, the shaft and barrelengineered with certain screw elements (e.g., shapes and clearances) toadjust the shearing profile. A typical RPM range for single screwextruder is about 10 to about 120. The single screw extruder design iscomposed of a feed section, compression section and metering section. Inthe feed section, using fairly high void volume flights, the polymer isheated and supplied into the compression section, where the melting iscompleted and the fully molten polymer is sheared. In the compressionsection, the void volume between the flights is reduced. In the meteringsection, the polymer is subjected to its highest shearing amount usinglow void volume between flights. For this work, general purpose singlescrew designs were used. In this unit, a continuous or steady state typeof process is achieved where the composition components are introducedat desired locations, and then subjected to temperatures and shearwithin target zones. The process can be considered to be a steady stateprocess as the physical nature of the interaction at each location inthe single screw process is constant as a function of time. This allowsfor optimization of the mixing process by enabling a zone-by-zoneadjustment of the temperature and shear, where the shear can be changedthrough the screw elements and/or barrel design or screw speed.

The mixed composition exiting the single screw extruder can then bepelletized via extrusion of the melt into a liquid cooling medium, oftenwater, and then the polymer strand can be cut into small pieces orpellets. Alternatively, the mixed composition can be used to produce thefinal formed structure, for example fibers. There are two basic types ofmolten polymer pelletization process used in polymer processing: strandcutting and underwater pelletization. In strand cutting the compositionis rapidly quenched (generally much less than 10 seconds) in the liquidmedium then cut into small pieces. In the underwater pelletizationprocess, the molten polymer is cut into small pieces then simultaneouslyor immediately thereafter placed in the presence of a low temperatureliquid which rapidly quenches and crystallizes the polymer. Thesemethods are commonly known and used within the polymer processingindustry.

The polymer strands that come from the extruder are rapidly placed intoa water bath, most often having a temperature range of 1° C. to 50° C.(e.g., normally is about room temperature, which is 25° C.). Analternate end use for the mixed composition is further processing intothe desired structure, for example fiber spinning, films or injectionmolding. The single screw extrusion process can provide for a high levelof mixing and high quench rate. A single screw extruder also can be usedto further process a pelletized composition into fibers and injectionmolded articles. For example, the fiber single screw extruder can be a37 mm system with a standard general purpose screw profile and a 30:1length to diameter ratio.

Twin Screw Extruder: A twin screw extruder is the typical unit used inmost molten polymer extrusion, where high intensity mixing is required.The twin screw extruder includes two shafts and an outer barrel. Atypical RPM range for twin screw extruder is about 10 to about 1200. Thetwo shafts can be co-rotating or counter rotating and allow for closetolerance, high intensity mixing. In this type of unit, a continuous orsteady state type of process is achieved where the compositioncomponents are introduced at desired locations along the screws, andsubjected to high temperatures and shear within target zones. Theprocess can be considered to be a steady state process as the physicalnature of the interaction at each location in the single screw processis constant as a function of time. This allows for optimization of themixing process by enabling a zone-by-zone adjustment of the temperatureand shear, where the shear can be changed through the screw elementsand/or barrel design.

The mixed composition at the end of the twin screw extruder can then bepelletized via extrusion of the melt into a liquid cooling medium, oftenwater, and then the polymer strand is cut into small pieces or pellets.Alternatively, the mixed composition can be used to produce the finalformed structure, for example fibers. There are two basic types ofmolten polymer pelletization process, strand cutting and underwaterpelletization, used in polymer processing. In strand cutting thecomposition is rapidly quenched (generally much less than 10s) in theliquid medium then cut into small pieces. In the underwaterpelletization process, the molten polymer is cut into small pieces thensimultaneously or immediately thereafter placed in the presence of a lowtemperature liquid which rapidly quenches and crystallizes the polymer.An alternate end use for the mixed composition is direct furtherprocessing into filaments or fibers via spinning of the molten admixtureaccompanied by cooling.

Three different screw profiles can be employed using a Baker PerkinsCT-25 25 mm corotating 40:1 length to diameter ratio system. Thisspecific CT-25 is composed of nine zones where the temperature can becontrolled, as well as the die temperature. Four liquid injection sitesas also possible, located between zone 1 and 2 (location A), zone 2 and3 (location B), zone 4 and 5 (location C). and zone 6 and 7 (locationD).

The liquid injection location is not directly heated, but indirectlythrough the adjacent zone temperatures. Locations A, B, C and D can beused to inject the additive. Zone 6 can contain a side feeder for addingadditional solids or used for venting. Zone 8 contains a vacuum forremoving any residual vapor, as needed. Unless noted otherwise, themelted wax is injected at location A. The wax is melted via a glue tankand supplied to the twin-screw via a heated hose. Both the glue tank andthe supply hose are heated to a temperature greater than the meltingpoint of the wax (e.g., about 80° C.).

Two types of regions, conveyance and mixing, are used in the CT-25. Inthe conveyance region, the materials are heated (including throughmelting which is done in Zone 1 into Zone 2 if needed) and conveyedalong the length of the barrel, under low to moderate shear. The mixingsection contains special elements that dramatically increase shear andmixing. The length and location of the mixing sections can be changed asneeded to increase or decrease shear as needed.

Two primary types of mixing elements are used for shearing and mixing.The first are kneading blocks and the second are thermal mechanicalenergy elements. The simple mixing screw has 10.6% of the total screwlength using mixing elements composed of kneading blocks in a single setfollowed by a reversing element. The kneading elements are RKB 45/5/12(right handed forward kneading block with 45° offset and five lobes at12 mm total element length), followed by two RKB 45/5/36 (right handedforward kneading block with 45° offset and five lobes at 36 mm totalelement length), that is followed by two RKB 45/5/12 and reversingelement 24/12 LH (left handed reversing element 24 mm pitch at 12 mmtotal element length).

The Simple mixing screw mixing elements are located in zone 7. TheIntensive screw is composed of additional mixing sections, four intotal. The first section is single set of kneading blocks is a singleelement of RKB45/5/36 (located in zone 2) followed by conveyanceelements into zone 3 where the second mixing zone is located. In thesecond mixing zone, two RKB 45/5/36 elements are directly followed byfour TME 22.5/12 (thermomechanical element with 22.5 teeth perrevolution and total element length of 12 mm) then two conveyanceelements into the third mixing area. The third mixing area, located atthe end of zone 4 into zone 5, is composed of three RKB 45/5/36 and aKB45/5/12 LH (left handed forward reversing block with 45° offset andfive lobes at 12 mm total element length. The material is conveyedthrough zone 6 into the final mixing area comprising two TME 22.5/12,seven RKB 45/5/12, followed by SE 24/12 LH. The SE 24/12 LH is areversing element that enables the last mixing zone to be completelyfilled with polymer and additive, where the intensive mixing takesplace. The reversing elements can control the residence time in a givenmixing area and are a key contributor to the level of mixing.

The High Intensity mixing screw is composed of three mixing sections.The first mixing section is located in zone 3 and is two RKB45/5/36followed by three TME 22.5/12 and then conveyance into the second mixingsection. Prior to the second mixing section three RSE 16/16 (righthanded conveyance element with 16 mm pitch and 16 mm total elementlength) elements are used to increase pumping into the second mixingregion. The second mixing region, located in zone 5, is composed ofthree RKB 45/5/36 followed by a KB 45/5/12 LH and then a full reversingelement SE 24/12 LH. The combination of the SE 16/16 elements in frontof the mixing zone and two reversing elements greatly increases theshear and mixing. The third mixing zone is located in zone 7 and iscomposed of three RKB 45/5/12, followed by two TME 22.5.12 and thenthree more RKB45/5/12. The third mixing zone is completed with areversing element SE 24/12 LH.

An additional screw element type is a reversing element, which canincrease the filling level in that part of the screw and provide bettermixing. Twin screw compounding is a mature field. One skilled in the artcan consult books for proper mixing and dispersion. These types of screwextruders are well understood in the art and a general description canbe found in: Twin Screw Extrusion 2E: Technology and Principles by JamesWhite from Hansen Publications. Although specific examples are given formixing, many different combinations are possible using various elementconfigurations to achieve the needed level of mixing.

Properties of Compositions

The compositions as disclosed herein can have one or more of thefollowing properties that provide an advantage over known thermoplasticcompositions. These benefits can be present alone or in a combination.

Shear Viscosity Reduction: As shown in FIG. 1, addition of the wax,e.g., HSBO, to the thermoplastic polymer, e.g., Basell PH-835, reducesthe viscosity of the thermoplastic polymer (here, polypropylene in thepresence of the molten HSBO wax). Viscosity reduction is a processimprovement as it can allow for effectively higher polymer flow rates byhaving a reduced process pressure (lower shear viscosity), or can allowfor an increase in polymer molecular weight, which improves the materialstrength. Without the presence of the wax, it may not be possible toprocess the polymer with a high polymer flow rate at existing processconditions in a suitable way.

Sustainable Content: Inclusion of sustainable materials into theexisting polymeric system is a strongly desired property. Materials thatcan be replaced every year through natural growth cycles contribute tooverall lower environmental impact and are desired.

Pigmentation: Adding pigments to polymers often involves using expensiveinorganic compounds that are particles within the polymer matrix. Theseparticles are often large and can interfere in the processing of thecomposition. Using a wax as disclosed herein, because of the finedispersion (as measured by droplet size) and uniform distributionthroughout the thermoplastic polymer allows for coloration, such as viatraditional ink compounds. Soy ink is widely used in paper publication)that does not impact processability.

Fragrance: Because the waxes, for example HSBO, can contain perfumesmuch more preferentially than the base thermoplastic polymer, thepresent composition can be used to contain scents that are beneficialfor end-use. Many scented candles are made using SBO based or paraffinbased materials, so incorporation of these into the polymer for thefinal composition is useful.

Surface Feel: The presence of the wax can change the surface propertiesof the composition, compared to a thermoplastic polymer compositionwithout a wax, making it feel softer.

Morphology: The benefits are delivered via the morphology produced inproduction of the compositions. The morphology is produced by acombination of intensive mixing and rapid crystallization. The intensivemixing comes from the compounding process used and rapid crystallizationcomes from the cooling process used. High intensity mixing is desiredand rapid crystallization is used to preserves the fine pore size andrelatively uniform pore size distribution. FIG. 2 shows HSBO in BasellProfax PH-835, with the small pore sizes of less than 10 μm, less than 5μm, and less than 1 μm.

Improved Spinning Performance: Adding the wax has shown to improvespinning of fibers, enabling a finer diameter filament to be achieved vsthe neat polymer the additive has been admixed into during compositionpreparation.

Processes for Making Fibers

Fibers can be spun from a melt of the compositions as disclosed herein.In melt spinning, there is no mass loss in the extrudate. Melt spinningis differentiated from other spinning, such as wet or dry spinning fromsolution, where a solvent is being eliminated by volatilizing ordiffusing out of the extrudate resulting in a mass loss.

Spinning can occur at 120° C. to about 320° C., preferably 185° C. toabout 250° C. and most preferably from 200° C. to 230° C. Fiber spinningspeeds of greater than 100 meters/minute are preferred. Preferably, thefiber spinning speed is about 1,000 to about 10,000 meters/minute, morepreferably about 2,000 to about 7,000 meters/minute, and most preferablyabout 2,500 to about 5,000 meters/minute. The polymer composition isspun fast to avoid brittleness in the fiber.

Continuous filaments or fibers can be produced through spunbond methods.Essentially continuous or essentially discontinuous filaments or fiberscan be produced through melt fibrillation methods such as meltblowing ormelt film fibrillation processes. Alternatively, non-continuous (staplefibers) fibers can be produced. The various methods of fibermanufacturing can also be combined to produce a combination technique.

The homogeneous blend can be melt spun into monocomponent ormulticomponent fibers on conventional melt spinning equipment. Theequipment will be chosen based on the desired configuration of themulticomponent. Commercially available melt spinning equipment isavailable from Hills, Inc. located in Melbourne, Fla. The temperaturefor spinning is about 100° C. to about 320° C. The processingtemperature is determined by the chemical nature, molecular weights andconcentration of each component. The fibers spun can be collected usingconventional godet winding systems or through air drag attenuationdevices. If the godet system is used, the fibers can be further orientedthrough post extrusion drawing at temperatures of about 25° C. to about200° C. The drawn fibers may then be crimped and/or cut to formnon-continuous fibers (staple fibers) used in a carding, airlaid, orfluidlaid process.

For example, a suitable process for spinning bicomponent sheath corefibers using the composition in the sheath and a different compositionin the core is as follows. A composition is first prepared throughcompounding containing 10 wt % HSBO and a second composition is firstprepared through compounding containing 30 wt % HSBO. The 10 wt % HSBOcomponent extruder profile may be 180° C., 200° C. and 220° C. in thefirst three zones of a three heater zone extruder. The transfer linesand melt pump heater temperatures may be 220° C. for the firstcomposition. The second composition extruder temperature profile can be180° C., 230° C. and 230° C. in the first three zones of a three heaterzone extruder. The transfer lines and melt pump can be heated to 230° C.In this case, the spinneret temperature can be 220° C. to 230° C.

Fine Fiber Production

In one embodiment, the homogenous blend is spun into one or morefilaments or fibers by melt film fibrillation. Suitable systems and meltfilm fibrillation methods are described in U.S. Pat. Nos. 6,315,806,5,183,670, and 4,536,361, to Torobin et al., and U.S. Pat. Nos.6,382,526, 6,520,425, and 6,695,992, to Reneker et al. and assigned tothe University of Akron. Other melt film fibrillation methods andsystems are described in the U.S. Pat. Nos. 7,666,343 and 7,931,457, toJohnson, et al., U.S. Pat. No. 7,628,941, to Krause et al., and U.S.Pat. No. 7,722,347, to Krause, et al. Methods and apparatus described inabove patents provide nonwoven webs with uniform and narrow fiberdistribution, reduced or minimal fiber defects. Melt film fibrillationprocess comprises providing one or more melt films of the homogenousblend, one or more pressurized fluid streams (or fiberizing fluidstreams) to fibrillate the melt film into ligaments, which areattenuated by the pressurized fluid stream. Optionally, one or morepressurized fluid streams may be provided to aid the attenuation andquenching of the ligaments to form fibers. Fibers produced from the meltfilm fibrillation process using one of embodiment homogenous blend wouldhave diameters typically ranging from about 100 nanometer (0.1micrometer) to about 5000 nanometer (5 micrometer). In one embodiment,the fibers produced from the melt film fibrillation process of thehomogenous blend would be less than 2 micrometer, more preferably lessthan 1 micrometer (1000 nanometer), and most preferably in the range of100 nanometer (0.1 micrometer) to about 900 nanometer (0.9 micrometer).The average diameter (an arithmetic average diameter of at least 100fiber samples) of fibers of the homogenous blend produced using the meltfilm fibrillation would be less than 2.5 micrometer, more preferablyless than 1 micrometer, and most preferably less than 0.7 micrometer(700 nanometer). The median fiber diameter can be 1 micrometer or less.In an embodiment, at least 50% of the fibers of the homogenous blendproduced by the melt film fibrillation process may have diameter lessthan 1 micrometer, more preferably, at least 70% of the fibers may havediameter less than 1 micrometer, and most preferably, at least 90% ofthe fibers may have diameter less than 1 micrometer. In certainembodiments, even 99% or more fibers may have diameter less than 1micrometer when produced using the melt film fibrillation process.

In the melt film fibrillation process, the homogenous blend is typicallyheated until it forms a liquid and flows easily. The homogenous blendmay be at a temperature of from about 120° C. to about 350° C. at thetime of melt film fibrillation, in one embodiment from about 160° C. toabout 350° C., and in another embodiment from about 200° C. to about300° C. The temperature of the homogenous blend depends on thecomposition. The heated homogenous blend is at a pressure from about 15pounds per square inch absolute (psia) to about 400 psia, in anotherembodiment from about 20 psia to about 200 psia, and in yet anotherembodiment from about 25 psia to about 100 psia.

Non-limiting examples of the pressurized fiberizing fluid stream aregases such as air or nitrogen or any other fluid compatible (defined asreactive or inert) with homogenous blend composition. The fiberizingfluid stream can be at a temperature close to the temperature of theheated homogenous blend. The fiberizing fluid stream temperature may beat a higher temperature than the heated homogenous blend to help in theflow of the homogenous blend and the formation of the melt film. In oneembodiment, the fiberizing fluid stream temperature is about 100° C.above the heated homogenous blend, in another embodiment about 50° C.above the heated homogenous blend, or just at temperature of the heatedhomogenous blend. Alternatively, the fiberizing fluid stream temperaturecan be below the heated homogenous blend temperature. In one embodiment,the fiberizing fluid stream temperature is about 50° C. below the heatedhomogenous blend, in another embodiment about 100° C. below the heatedhomogenous blend, or 200° C. below heated homogenous blend. In certainembodiments, the temperature of the fiberizing fluid stream may beranging from about −100° C. to about 450° C., more preferably, rangingfrom about −50° C. to 350° C., and most preferably, ranging from about0° C. to about 300° C. The pressure of the fiberizing fluid stream issufficient to fibrillate the homogenous blend into fibers, and is abovethe pressure of the heated homogenous blend. The pressure of thefiberizing fluid stream may range from about 15 psia to about 500 psia,more preferably from about 30 psia to about 200 psia, and mostpreferably from about 40 psia to about 100 psia. The fiberizing fluidstream may have a velocity of more than about 200 meter per second atthe location of melt film fibrillation. In one embodiment, at thelocation of melt film fibrillation, the fiberizing fluid stream velocitywill be more than about 300 meter per second, i.e., transonic velocity;in another embodiment more than about 330 meter per second, i.e., sonicvelocity; and in yet another embodiment from about 350 to about 900meters per second (m/s), i.e., supersonic velocity from about Mach 1 toMach 3. The fiberizing fluid stream may pulsate or may be a steady flow.The homogenous blend throughput will primarily depend upon the specifichomogenous blend used, the apparatus design, and the temperature andpressure of the homogenous blend. The homogenous blend throughput willbe more than about 1 gram per minute per orifice, for example in acircular nozzle. In one embodiment, the homogenous blend throughput willbe more than about 10 gram per minute per orifice and in anotherembodiment greater than about 20 gram per minute per orifice, and in yetanother embodiment greater than about 30 gram per minute per orifice. Inan embodiment with the slot nozzle, the homogenous blend throughput willbe more than about 0.5 kilogram per hour per meter width of the slotnozzle. In another slot nozzle embodiment, the homogenous blendthroughput will be more than about 5 kilogram per hour per meter widthof the slot nozzle, and in another slot nozzle embodiment, thehomogenous blend throughput will be more than about 20 kilogram per hourper meter width of the slot nozzle, and in yet another slot nozzleembodiment, the homogenous blend throughput will be more than about 40kilogram per hour per meter width of the slot nozzle. In certainembodiments of the slot nozzle, the homogenous blend throughput mayexceed about 60 kilogram per hour per meter width of the slot nozzle.There will likely be several orifices or nozzles operating at one timewhich further increases the total production throughput. The throughput,along with pressure, temperature, and velocity, are measured at theorifice or nozzle for both circular and slot nozzles.

Optionally, an entraining fluid can be used to induce a pulsating orfluctuating pressure field to help in forming fibers. Non-limitingexamples of the entraining fluid are pressurized gas stream such ascompressed air, nitrogen, oxygen, or any other fluid compatible (definedas reactive or inert) with the homogenous blend composition. Theentertaining fluid with a high velocity can have a velocity near sonicspeed (i.e. about 330 m/s) or supersonic speeds (i.e. greater than about330 m/s). An entraining fluid with a low velocity will typically have avelocity of from about 1 to about 100 m/s and in another embodiment fromabout 3 to about 50 m/s. It is desirable to have low turbulence in theentraining fluid stream 14 to minimize fiber-to-fiber entanglements,which usually occur due to high turbulence present in the fluid stream.The temperature of the entraining fluid 14 can be the same as the abovefiberizing fluid stream, or a higher temperature to aid quenching offilaments, and ranges from about −40° C. to 40° C. and in anotherembodiment from about 0° C. to about 25° C. The additional fluid streammay form a “curtain” or “shroud” around the filaments exiting from thenozzle. Any fluid stream may contribute to the fiberization of thehomogenous blend and can thus generally be called fiberizing fluidstream.

The spunlaid processes disclosed herein use a high speed spinningprocess as disclosed in U.S. Pat. Nos. 3,802,817; 5,545,371; 6,548,431and 5,885,909. In these melt spinning processes, extruders supply moltenpolymer to melt pumps, which deliver specific volumes of molten polymerthat transfer through a spinpack, composed of a multiplicity ofcapillaries formed into fibers, where the fibers are cooled through anair quenching zone and are pneumatically drawn down to reduce their sizeinto highly attenuated fibers to increase fiber strength throughmolecular level fiber orientation. The drawn fibers are then depositedonto a porous belt, often referred to as a forming belt or formingtable.

Spunlaid Process

The fibers forming the base substrate disclosed herein are preferablycontinuous filaments forming spunlaid fabrics. Spunlaid fabrics aredefined as unbonded fabrics having basically no cohesive tensileproperties formed from essentially continuous filaments. Continuousfilaments are defined as fibers with high length to diameter ratios,with a ratio of more than 10,000:1. Continuous filaments that composethe spunlaid fabric are not staple fibers, short cut fibers or otherintentionally made short length fibers. The continuous filaments,defined as essentially continuous, are on average, more than 100 mmlong, preferably more than 200 mm long. The continuous filaments arealso not crimped, intentionally or unintentionally. Essentiallydiscontinuous fibers and filaments are defined as having a length lessthan 100 mm long, preferably less than 50 mm long.

The spunlaid processes can use a high speed spinning process asdisclosed in U.S. Pat. Nos. 3,802,817; 5,545,371; 6,548,431 and5,885,909. In these melt spinning processes, extruders supply moltenpolymer to melt pumps, which deliver specific volumes of molten polymerthat transfer through a spinpack, composed of a multiplicity ofcapillaries formed into fibers, where the fibers are cooled through anair quenching zone and are pneumatically drawn down to reduce their sizeinto highly attenuated fibers to increase fiber strength throughmolecular level fiber orientation. The drawn fibers are then depositedonto a porous belt, often referred to as a forming belt or formingtable.

In one embodiment, the spunlaid process used to make the continuousfilaments will contain 100 to 10,000 capillaries per meter, preferably200 to 7,000 capillaries per meter, more preferably 500 to 5,000capillaries per meter. The polymer mass flow rate per capillary in thepresent invention will be greater than 0.3 GHM (grams per hole perminute). The preferred range is from 0.35 GHM to 2 GHM, preferablybetween 0.4 GHM and 1 GHM, still more preferred between 0.45 GHM and 8GHM and the most preferred range from 0.5 GHM to 0.6 GHM.

The spunlaid process can contain a single process step for making thehighly attenuated, uncrimped continuous filaments. Extruded filamentsare drawn through a zone of quench air where they are cooled andsolidified as they are attenuated. Such spunlaid processes are disclosedin U.S. Pat. No. 3,338,992, U.S. Pat. No. 3,802,817, U.S. Pat. No.4,233,014 US 5,688,468, U.S. Pat. No. 6,548,431 B1, U.S. Pat. No.6,908,292 B2 and U.S. Application 2007/0057414A1. The technologydescribed in EP 1,340,843 B1 and EP 1 323,852 B1 can also be used toproduce the spunlaid nonwovens. The highly attenuated continuousfilaments are directly drawn down from the exit of the polymer from thespinneret to the attenuation device, wherein the continuous filamentdiameter or denier does not change substantially as the spunlaid fabricis formed on the forming table

Preferred polymeric materials include, but are not limited to,polypropylene and polypropylene copolymers, polyethylene andpolyethylene copolymers, polyester and polyester copolymers, polyamide,polyimide, polylactic acid, polyhydroxyalkanoate, polyvinyl alcohol,ethylene vinyl alcohol, polyacrylates, and copolymers thereof andmixtures thereof, as well as the other mixture disclosed herein. Othersuitable polymeric materials include thermoplastic starch compositionsas described in detail in U.S. publications 2003/0109605A1 and2003/0091803. Still other suitable polymeric materials include ethyleneacrylic acid, polyolefin carboxylic acid copolymers, and combinationsthereof. The polymers described in U.S. Pat. No. 6,746,766, U.S. Pat.No. 6,818,295, U.S. Pat. No. 6,946,506 and US Published Application03/0092343. Common thermoplastic polymer fiber grade materials arepreferred, most notably polyester based resins, polypropylene basedresins, polylactic acid based resin, polyhydroxyalkonoate based resin,and polyethylene based resin and combination thereof. Most preferred arepolyester and polypropylene based resins.

It should also be noted that the ability to utilize mixture compositionsabove 40 weigh percent (wt %) wax in the extrusion process, where themasterbatch level of wax is combined with a lower concentration (down to0 wt %) thermoplastic composition during extrusion to produce a waxcontent within the target range.

In the process of spinning fibers, particularly as the temperature isincreased above 105° C., typically it is desirable for residual waterlevels to be 1%, by weight of the fiber, or less, alternately 0.5% orless, or 0.15% or less.

Articles

The fibers can be converted to nonwovens by different bonding methods.Continuous fibers can be formed into a web using industry standardspunbond type technologies while staple fibers can be formed into a webusing industry standard carding, airlaid, or wetlaid technologies.Typical bonding methods include: calender (pressure and heat), thru-airheat, mechanical entanglement, hydrodynamic entanglement, needlepunching, and chemical bonding and/or resin bonding. The calender,thru-air heat, and chemical bonding are the preferred bonding methodsfor the starch polymer fibers. Thermally bondable fibers are requiredfor the pressurized heat and thru-air heat bonding methods.

The fibers that are made with any of the compositions discussed hereinmay also be bonded or combined with other synthetic or natural fibers tomake disposable articles. The synthetic or natural fibers may be blendedtogether in the forming process or used in discrete layers. Suitablesynthetic fibers include fibers made from polypropylene, polyethylene,polyester, polyacrylates, and copolymers thereof and mixtures thereof.Natural fibers include cellulosic fibers and derivatives thereof.Suitable cellulosic fibers include those derived from any tree orvegetation, including hardwood fibers, softwood fibers, hemp, andcotton. Also included are fibers made from processed natural cellulosicresources such as rayon.

The fibers that are made with any of the compositions discussed hereinmay be used to make one or more layers of nonwoven that can then be usedto make a disposable article. The nonwoven described herein may becombined with additional nonwovens or films to produce a laminate usedeither by itself or as a component in a complex combination of othermaterials, such as a baby diaper or feminine care pad. Disposablearticles that may benefit from the use of the fibers and nonwovensdescribed herein include disposable absorbent articles such as babydiapers, training pants, adult incontinence articles, panty liners,sanitary napkins, tampons, absorbent pads (such as the SWIFFER WET andSWIFFER WETJET pads). A typical absorbent article that may include atleast one layer of a nonwoven comprising fibers that are made with anyof the compositions discussed herein is schematically represented inFIG. 3. The disposable absorbent article 10 includes a liquid perviouslayer 110, a liquid impervious layer 210 and an absorbent core 310disposed between the liquid pervious and impervious layers. In oneembodiment, fibers that are made with any of the compositions discussedherein are included (preferably in the form of a nonwoven layer) in atleast one of the liquid pervious layer, the liquid impervious layer, andthe absorbent core of a disposable absorbent article. In anotherembodiment, fibers that are made with any of the compositions discussedherein are included in at least one of the layers that form a cleaningwipe suitable to cleaning soft or hard surfaces. Other disposablearticles include filters for air, oil and water; vacuum cleaner filters;furnace filters; face masks; coffee filters, tea or coffee bags; thermalinsulation materials and sound insulation materials. The fibrous web mayalso include odor absorbents, termite repellants, insecticides,rodenticides, and the like, for specific uses. The resultant productabsorbs water and oil and may find use in oil or water spill clean-up,or controlled water retention and release for agricultural orhorticultural applications. The resultant fibers or fiber webs may alsobe incorporated into other materials such as saw dust, wood pulp,plastics, and concrete, to form composite materials, which can be usedas building materials such as walls, support beams, pressed boards, drywalls and backings, and ceiling tiles; other medical uses such as casts,splints, and tongue depressors; and in fireplace logs for decorativeand/or burning purpose.

EXAMPLES

Polymers: The primary polymers used in this work are polypropylene (PP)and polyethylene (PE), but other polymers can be used (see, e.g., U.S.Pat. No. 6,783,854, which provides a comprehensive list of polymers thatare possible, although not all have been tested). Specific polymersevaluated were:

-   -   Basell Profax PH-835: Produced by Lyondell-Basell as nominally a        35 melt flow rate Ziegler-Natta isotactic polypropylene.    -   Exxon Achieve 3854: Produced by Exxon-Mobil Chemical as        nominally a 25 melt flow rate metallocene isotactic        polypropylene.    -   Total 8650: Produced by Total Chemicals as a nominally 10 melt        flow rate Ziegler-Natta isotactic ethylene random copolymer        polypropylene.    -   Danimer 27510: Proprietary polyhydroxyalkanoate copolymer.    -   Dow Aspun 6811A: Produced by Dow Chemical as a 27 melt index        polyethylene copolymer.    -   BASF Ultramid B27: Produced by BASF as a low viscosity        polyamide-6 resin.    -   Eastman 9921: Produced by Eastman Chemical as a copolyester        terephthalic homopolymer with a nominally 0.81 intrinsic        viscosity.    -   Natureworks Ingeo Biopolymer 4032D: Produced by Natureworks as        polylactic acid polymer.

Waxes: Specific examples used were: Hydrogenated Soy Bean Oil (HSBO);Partially Hydrogenated Soy Bean Oil (HSBO); Partially Hydrogenated PalmKernel Oil (PKPKO); a commercial grade soy bean oil based-wax candlewith pigmentation and fragrance; standard green Soy Bean Green InkPigment

Compositions were made using a Baker Perkins CT-25 Screw, with the zonesset as noted in Table 1. Table 1 is shown in FIGS. 4-6.

Examples 1-26 and 42-46 were made using polypropylene resins, whileexamples 27-41 were made using other types of thermoplastic polymerresins. All examples successfully formed pellets, except examples 34, 37and 44. A slight excess of the wax was noted for examples 9, 12, and 27,e.g., small amounts of surging were noted at the outlet of thetwin-screw, but not sufficient to break the strand and disrupt theprocess. The slight excess of wax indicates that the level of mixing isinsufficient at that level or the polymer/wax composition is close tosaturation. Examples 43 and 44 also included an added pigment andperfume to the wax.

Examples 1-46 show the polymer plus additive tested in a stable rangeand to the limit. As used herein, stable refers to the ability of thecomposition to be extruded and to be pelletized. What was observed wasthat during the stable composition, strands from the B&P 25 mm systemcould be extruded, quenched in a water bath at 5° C. and cut via apelletizer without interruption. The twin-screw extrudate wasimmediately dropped into the water bath.

During stable extrusion, no significant amount of wax separated from theformulation strand (>99 wt % made it through the pelletizer). Saturationof the composition can be noted by separation of the polymer and waxfrom each other at the end of the twin-screw. The saturation point ofthe wax in the composition can change based on the wax and polymercombination, along with the process conditions. The practical utility isthat the wax and polymer remain admixed and do not separate, which is afunction of the mixing level and quench rate for proper dispersion ofthe additive. Specific Examples where the extrusion became unstable fromhigh wax inclusion are Example 34, 37, and 41.

Example 42 was processed using 30 wt % HSBO plus the addition of a scentand pigment (e.g., Febreze Rosewood scent and pigmented candle). Onecandle was added per 20 lb of wax into the glue tank and stirredmanually. The candle wick was removed before addition. The candlecontained both a pigment and perfume that were present in the as-formedpellets of the composition at the end of the process. Example 43 wasidentical to Example 42 except the vacuum was turned on to determine howmuch perfume or volatiles could be removed. No difference betweenas-formed pellets of Example 42 and Example 43 could be observed.

Examples 1-45 show the polymer plus additive tested in a stable rangeand to the limit. As used herein, stable refers to the ability of thecomposition to be extruded and to be pelletized. What was observed wasthat during the stable composition, strands from the B&P 25 mm systemcould be extruded, quenched in a water bath at 5° C. and cut via apelletizer without interruption. The twin-screw extrudate wasimmediately dropped into the water bath. During stable extrusion, nosignificant amount of oil separated from the formulation strand (>99 wt% made it through the pelletizer). The composition became unstable whenit was clear that the polymer and oil were separating from each other atthe end of the twin-screw and the composition strands could not bemaintained. Without being bound by theory, the polymer at this point isconsidered fully saturated. The saturation point can change based on theoil and polymer combination, along with the process conditions. Thepractical utility is that the oil and polymer remain admixed and do notseparate, which is a function of the mixing level and quench rate forproper dispersion of the additive. Specific Examples where the extrusionbecame unstable from high oil inclusion are Example 5, 7, 10, 12, 16 and42.

Fibers can be produced by melt spinning a composition of any one ofExamples 1-45. Fibers were melt spun with several composition examples.

The specific melt spinning equipment was a specially designedbicomponent extrusion system that consists of two single extruders,followed by a melt pump after each extruder. The two melt streams arecombined into a sheath/core spinpack purchased from Hills Inc. Thespinpack had 144 holes with capillary orifice diameter of 0.35 mm. Thefibers extruded through the spinpack were quenched on two sides using alm long quench system that blows air. The fibers are attenuated using ahigh pressure aspirator that draws the filaments down. The as-spunfibers were deposited onto a belt and collected to measure the finalas-spun filament diameter. The as-spun filament diameter is an averageof 10 measurements made under a light microscope. The reported fiberdiameter is the minimum fiber diameter that could be achieved withoutany filament breaks over five minutes for the entire 144 filaments beingextruded. The mass throughput used was 0.5 grams per capillary perminute (ghm). The specific fibers made and the processes for making themare shown in Table 2. Table 2 is shown in FIGS. 7 and 8.

Examples 47-65 show the results from producing useful fibers and thebenefit of improved spinnability by adding wax. The examples show thatutilizing polypropylene with wax in the core or into the sheath and coreimprove the spinnability and enable finer filaments to be produced.Finer fibers can improve softness, barrier properties and wickingbehavior.

Spunbond nonwovens were made by using the porous collection belt andadjusting the belt speed to target 20 grams per square meter (gsm). Thecollected fibers were first passed through a heated press roll at 100°C. at 50 PLI (pounds per linear inch) and then a heated calenderingsystem for the final thermal point bonding, followed by winding thecontinuous spunbond nonwoven onto a roll for later propertymeasurements. The heated calendering system consisted of a heatedengraved roll and heated smooth roll. The heated engraved roll had 18%raised bonding area. The calender roll pressure was held constant at 350PLI and the line speed of the forming belt was held constant at 38meters per minute.

The tensile properties of base substrates and structured substrates wereall measured the same way. The gauge width is 50 mm, gauge length is 100mm in the MD and 50 mm in the CD and the extension rate is 100 mm/min.The values reported are for strength and elongation at peak, unlessstated otherwise. Separate measurements are made for the MD and CDproperties. The typical units are Newton (N), and they are Newtons percentimeter (N/cm). The values presented are the average of at least tenmeasurements. The perforce load is 0.2 N. The samples should be storedat 23±2° C. and at 50±2% relative humidity for 24 hours with nocompression, then tested at 23±2° C. and at 50±2%. The tensile strengthas reported here is the peak tensile strength in the stress-straincurve. The elongation at tensile peak is the percent elongation at whichthe tensile peak is recorded.

Examples 66-105 show that useful spunbond nonwovens can be produced. Thespecifics of Examples 64-103 are shown in Table 3. Table 3 is shown inFIGS. 9 ad 10. The examples show that an optimum bonding temperature isto achieve at a particular fiber composition.

The dimensions and values disclosed herein are not to be understood asbeing strictly limited to the exact numerical values recited. Instead,unless otherwise specified, each such dimension is intended to mean boththe recited value and a functionally equivalent range surrounding thatvalue. For example, a dimension disclosed as “40 mm” is intended to mean“about 40 mm”. Every document cited herein, including any crossreferenced or related patent or application, is hereby incorporatedherein by reference in its entirety unless expressly excluded orotherwise limited. The citation of any document is not an admission thatit is prior art with respect to any invention disclosed or claimedherein or that it alone, or in any combination with any other referenceor references, teaches, suggests or discloses any such invention.Further, to the extent that any meaning or definition of a term in thisdocument conflicts with any meaning or definition of the same term in adocument incorporated by reference, the meaning or definition assignedto that term in this document shall govern.

While particular embodiments of the invention have been illustrated anddescribed, it would be obvious to those skilled in the art that variousother changes and modifications can be made without departing from thespirit and scope of the invention. It is therefore intended to cover inthe appended claims all such changes and modifications that are withinthe scope of this invention.

What is claimed is:
 1. A material web comprising: a. a first fiber layercomprising a plurality of fibers, each of which comprising an intimateadmixture of a thermoplastic polymer, and a wax and/or oil, wherein atleast some of the wax and/or oil is exposed at an outer surface of thefibers, the first fiber layer having a first surface energy; and b. asecond layer that is adjacent to the first fiber layer, the second layercomprising a second surface energy, wherein the first surface energy ishigher than the second surface energy, wherein the plurality of fiberscomprise bicomponent fibers comprising a first component and a secondcomponent, and wherein the wax or oil concentration in the firstcomponent is different than the concentration of the wax or oil in thesecond component.
 2. The material web of claim 1, wherein thebicomponent fibers are arranged in a side-by-side configuration.
 3. Thematerial web of claim 1, wherein the bicomponent fibers are arranged ina core-sheath configuration.
 4. The material web of claim 1, wherein thematerial web comprises fine fibers having a diameter of from 0.1 micronsto about 5 microns.
 5. The material web of claim 1, wherein the waxand/or oil comprises a stearic acid.
 6. The material web of claim 1,wherein the wax and/or oil comprises a triglyceride.
 7. The material webof claim 1, wherein the the material web comprises a plurality of cardedstaple length crimped fibers.
 8. The material web of claim 1, whereinthe material web comprises a plurality of spunbond crimped fibers. 9.The material web of claim 1, wherein the second layer comprises a film.10. The material web of claim 1, wherein the film comprises asurfactant.
 11. The material web of claim 1, wherein the second layercomprises a plurality of fibers and wherein the plurality of fibers ofthe second layer comprise cellulosic fibers.
 12. The material web ofclaim 11, wherein the cellulosic fibers comprise rayon fibers.
 13. Thematerial web of claim 12, wherein the material web comprises mechanicalentanglement, hydrodynamic entanglement, or needle punching.
 14. Thematerial web of claim 1, further comprising an additive associated withthe wax and/or oil.
 15. The material web of claim 14, wherein theadditive is a perfume or a colorant.
 16. The material web of claim 1,wherein the plurality of fibers of the first fiber layer are crimped.17. The material web of claim 16, wherein the plurality of fibers of thefirst fiber layer are bicomponent fibers having a first component and asecond component, wherein the first component is different than thesecond component such that the difference in crystallinity causescrimping.
 18. The material web of claim 17, wherein the plurality offibers of the first fiber layer are spunbond.
 19. The material web ofclaim 17, wherein the plurality of fibers of the first fiber layer arecarded.